Lhrh antagonist peptides

ABSTRACT

The present invention is directed to a method for essentially complete oxidation of a concentrated liquor containing oxidizable organic matter. Each step of the method is performed under substantially superatmospheric pressure. Initially, the liquor is preheated to a temperature higher than about 10° C. below the boiling point of water at the substantially superatmospheric pressure. A feed formed of the concentrated liquor is then essentially completely oxidized at a temperature of at least 800° C. in the presence of a gas comprising at least sixty percent by volume of oxygen to form a suspension of a hot gas and a molten slag. The molten slag is separated from the hot gas before the slag is dissolved in water to form a brine. The separated hot gas is then cooled to a temperature below 250° C. by quenching with an aqueous liquid. Finally, the aqueous liquid is separated from the hot gas.

BACKGROUND OF THE INVENTION

[0001] 1. Field of the Invention

[0002] The present invention relates generally to a method of oxidizingwaste liquors and, more particularly, to a method for mineralisation byoxidation at substantially superatmospheric pressure of essentially allorganic matter present in a concentrated liquor that has been obtainedby evaporation of waste liquors.

[0003] 2. Description of the Related Art

[0004] Today, industries are striving to minimise environmental impact.A part of this impact is the discharge of contaminated effluent towaterways and the emission of polluted gases to the ambient air.

[0005] Industry effluent often contains organic substances in lowconcentrations and inorganic ions, derived from raw materials and fromchemicals introduced to the process. The organic matter is sedimented ordegraded in the receiving water systems, thus consuming the oxygen inthe water. Part of the organic matter is taken in by living organisms.Some of these substances may accumulate in living tissues and further inthe food chain. Some of the substances are poisonous. The bulk of theinorganic matter is dissolved salts, which are present in large amountsin the receiving water systems. One of these is sodium chloride, ofwhich there is 3 kg per m³ in the Baltic Sea and about 30 kg per m³ inthe oceans. The inorganic matter, however, may also include smallquantities of metal ions, which are considered harmful. These are mainlyheavy metals such as zinc, lead, copper and cadmium.

[0006] The gases formed in combustion processes generally contain highamounts of carbon dioxide and often sulphur and nitrogen oxides.Recently a lot of attention has been paid to the pyrolysis residues inthe gases, i.e., the so called polyaromatic hydrocarbons. Somechloro-organic substances contained in the flue gases are considered anenvironmental hazard even in very low concentrations.

[0007] Effluent as described above are formed in various processes,e.g., in the food industry, in the chemical industry, and in the forestindustry. Some of these liquors are very concentrated and contain largequantities of valuable chemicals so that they are evaporated and burnedfor chemical recovery. It is well-known that this is the case with pulpcooking liquors. However, pulp mill bleach plant effluent are so dilutedthat they are currently not evaporated nor combusted, even if such amethod is known, e.g., as disclosed in Finnish Patent No. 85293.

[0008] Similar waste waters are produced even in other processes of thewood-processing industry, e.g., in debarking; in thermomechanicalpulping for the production of TMP or CTMP pulp; and in the chemicalcooking of straw or other annual plants, such as bagasse and differentspecies of grasses.

[0009] Typically, these effluent contain less than 10 percent, oftenless than one percent, of dissolved material. The inorganic materialtypically accounts for about 10 to 50 percent of the total amount ofdissolved material.

[0010] The waste waters are discharged to rivers, lakes and seas. Incountries with stringent environmental rules and regulations this isdone after external biological treatment in aerated lagoons or inactivated sludge plants. In these plants the organic matter can, to somedegree but not completely, be decomposed or solidified for separation.The dissolved inorganic matter, especially heavy metals, remainuntouched. In principle, heavy metals could be separated from theeffluent by means of chemical precipitation. However, with very lowconcentrations of the inorganic matter, a complete precipitation can notbe achieved and the separation of the precipitated matter from largequantities of liquid is difficult.

[0011] Evaporation equipment for the concentration of even largeeffluent flows is currently commercially available. However, when theeffluent contains salts of limited solubility, a crystallization ofthese salts takes place when evaporating the liquors to a high drysolids content. As a result, the heat transfer surfaces of theevaporation equipment become fouled, and the evaporation capacity isreduced. This tendency becomes all the more apparent with higher targetconcentrations of the evaporated liquid. With evaporation, the effluentis separated into a condensate and a concentrate. The condensate can bereused in the process either as such or after further cleaning. Theconcentrate, which contains the bulk of the organic matter in theeffluent and nearly all of the inorganic matter, needs to be disposedof. The best way to do this is to completely oxidise the organic matterto carbon dioxide and water vapour and to separate the harmful metalsfrom the inorganic incineration residue.

[0012] There is equipment designed for incineration of concentrates thatare especially difficult to treat. Commercial applications are availablein many countries, e.g., as operated by Ekokem Oy in Finland. Also, someindustrial enterprises have incineration equipment of their own for thedisposal of hazardous waste. Characteristic of these installations isthat they operate at atmospheric pressure and use air as an oxidisingagent. To achieve a complete oxidation of all organic matter in theseconventional systems, a combustion temperature of at least 800° C. isrequired with a retention time of several seconds inside the combustionchamber. When incinerating liquids with high ash content, even if theyhave been evaporated to a high solids content, the necessary combustiontemperature can be reached only by using supplementary fuel. These typesof incineration furnaces are marketed by, e.g., Ahlstrom Corporation andJohn Zink Company Ltd.

[0013] Air contains only about 21% oxygen, the bulk of the remainderbeing inert nitrogen, which creates a ballast for the incineration. Withthis ballast, a considerable amount of energy is needed to increase thetemperature above 800° C. This is the primary reason why the furnacesneed fossil fuel, e.g., natural gas or fuel oil, to achieve and tomaintain the required combustion chamber temperature. Of course, thefossil fuel also requires combustion air, which further increases theamount of inert nitrogen passed through the combustion chamber and thesubsequent flue gas duct.

[0014] The specific volume of gases is high at high temperatures andatmospheric pressure. As a result, the combustion chamber becomes verybig, and the devices needed for cleaning and transporting the gas becomelarge and also expensive. For this reason, the treatment of diluteeffluent by evaporation and incineration has not become a commonpractice in the process industry.

[0015] It is generally known that the volume of gas at a giventemperature decreases as pressure increases. This relationship isutilised in, e.g., gasifiers, as disclosed in publications WO-93/022 andWO-93/09205. However, they deal with methods to gasify organic matter inreducing conditions and not with complete oxidation of this matter.

[0016] What is needed is an efffective method of simultaneously removingenvironmentally harmful organic and inorganic matter from effluentwithout the additional cost and complexity involved in adding fossilfuels and the like to the process.

SUMMARY OF THE INVENTION

[0017] The object of the present invention is to provide a method fortreating preconcentrated waste liquors by complete oxidation ofessentially all organic matter in the liquor to carbon dioxide and watervapour such that, at the same time, all harmful metals can beeffectively and efficiently separated from the inorganic incinerationresidue. This is accomplished in equipment that is substantially smallerand less expensive than the equipment now in use.

[0018] The present invention is directed to a method for essentiallycomplete oxidation of a concentrated liquor containing oxidizableorganic matter. Each step of the method is performed under substantiallysuperatmospheric pressure. Initially, the liquor is preheated to atemperature higher than about 10° C. below the boiling point of water atthe substantially superatmospheric pressure. A feed formed of theconcentrated liquor is then essentially completely oxidized at atemperature of at least 800° C. in the presence of a gas comprising atleast sixty percent by volume of oxygen to form a suspension of a hotgas and a molten slag. The molten slag is separated from the hot gasbefore the slag is dissolved in water to form a brine. The separated hotgas is then cooled to a temperature below 250° C. by quenching with anaqueous liquid. Finally, the aqueous liquid is separated from the hotgas.

[0019] In the context of the present invention, the following terms areused:

[0020] “slag”—the inorganic residue left after complete oxidation of thepreheated concentrated liquor;

[0021] “molten slag”—slag, the substantial part of which is in liquidphase;

[0022] “brine”—a solution formed when the slag is dissolved in water;

[0023] “solid residue”—the insoluble part of the slag when it isdissolved in water;

[0024] “quench liquid”—water or water containing only inorganic salts.

[0025] According to the present invention the oxidation of the preheatedconcentrated liquor takes place with a pressurised gas containing atleast 60 percent of oxygen, by volume, preferably pure oxygen, and theoxidation is carried out under substantially superatmospheric pressureand thus in devices small in volume.

[0026] In a preferred embodiment of the present invention, the method iscarried out at a superatmospheric pressure of at least 100 kPa,preferably from about 900 to about 1100 kPa. It is essential that theoxidation is conducted with pressurised gas containing a surplus ofoxygen in relation to the amount theoretically needed to completelyoxidise all organic matter in the final concentrate. The preferredoxygen content of the pressurized gas is close to 100 percent, byvolume, but the pressurised gas can be contaminated with other gases,e.g., nitrogen, carbon monoxide, or carbon dioxide. The content oforganic matter in the feed concentrate is chosen so that, when preheatedto the temperature required for oxidation, it is possible to maintain asufficient reaction temperature (at least 800° C., preferably 1000° C.)in the reaction chamber. At these temperatures the slag is in moltenstate.

[0027] According to the present invention, the molten slag is separatedfrom the gas before it is brought into contact with an aqueous quenchliquid. The molten slag is separated from the hot gas preferably byforce of gravitation and/or with centrifugal force, after which themolten slag is brought into contact with water. Heavy metals containedin the slag will form insoluble salts, mainly carbonates, which can beseparated from the brine formed when the slag is brought in contact withwater.

[0028] According to a preferred embodiment of the present invention, themolten slag is allowed to flow down through constriction, such as asmall passage to an agitated slag dissolving vessel, wherein water isintroduced in such quantities that the steam generated will suffice toprevent hot gas from entering the dissolving vessel through the passage.

BRIEF DESCRIPTION OF THE DRAWING

[0029] Other objects and features of the present invention will becomeapparent from the Detailed Description when read in light of theattached drawing. It is to be understood that this drawing is for thepurpose of illustration only and is not intended as a definition of thelimits of the invention.

[0030]FIG. 1 illustrates a schematic side-view of a device especiallysuitable for carrying out the method of this invention.

DETAILED DESCRIPTION

[0031] In the enclosed Figure, number 1 denotes a reaction chamber,which is under a superatmospheric pressure of at least of 100 kPa,preferably about 1000 kPa. The outer shell of the reaction chamber is apressure vessel 2 containing water with a pressure corresponding to thatof the reaction chamber 1. There is, therefore, no essential pressuredifference over the wall of reaction chamber 1. In reaction chamber 1there is a burner 3, to which the preheated concentrated liquor to beoxidised is pumped through a piping 12. Oxygen is fed to burner 3 with acompressor and through piping 13. If oxygen has a sufficient pressure inits storage tank, the compressor is unnecessary. The oxygen can becontaminated by other gases, e.g., by nitrogen. In the latter case theminimum oxygen content of the gas is 60 percent, by volume.

[0032] Inside reaction chamber 1 a minimum temperature of 800° C., andpreferably about 1000° C., is maintained, so that complete oxidation ofthe organic material is accomplished and all inorganic substances meltto form a molten slag. Some molten slag particles hit the inner surfacesof reactor 1 and flow down on them. The inner walls of reactor 1, builtof a suitable metal, can be furnished with fire-proof refractorymaterial. However, according to a preferred embodiment of the presentinvention, the reactor inner wall is not furnished with any refractorymaterial, but the reactor wall is effectively cooled with water. Suchcooling causes the slag to adhere to the wall and form a solidifiedlayer, thus reducing the heat transfer through the wall and protectingthe metal against corrosion.

[0033] The water inside pressure vessel 2 will partly vaporise. Themixture of water and steam is led to a steam drum 34 through duct 35. Indrum 34, the steam is separated from the water, and the water is fedback into pressure vessel 2 through duct 36.

[0034] It is not possible to maintain a stable continuous reaction inreaction chamber 1 unless the feed of the concentrated liquor is heatedto a temperature close to the boiling point of water at the reactionchamber pressure. Therefore the feed of the concentrated liquor isheated to a temperature higher than 10° C. below the boiling point ofwater at the reaction chamber pressure. According to a preferredembodiment of the present invention, this will take place in two steps,first indirectly in a steam-heated heat exchanger 30 and subsequently bydirect steam in a pressurised storage vessel 31. In order to obtain abig contact area between the incoming liquor and the steam, the liquoris fed through an atomising nozzle 32 into storage vessel 31 above theliquid level in this vessel. The liquor is pumped through piping 33. Thedevices are preferably designed so that a great proportion of theheating takes place in the heat exchanger, from which the condensate isextracted through pipe 37 and not mixed with the preheated concentratedliquor.

[0035] Steam to devices 30 and 31 is taken from drum 34 via pipe 39. Theamount of steam is balanced by external steam through a second pipe 38,or when there is a surplus of steam, by extracting it through a thirdpipe 40.

[0036] Because the reaction chamber shell is subject to almost nostress, it can be designed relatively freely. The lower part can bebuilt with a passage 4, through which a suspension of the gas and themolten slag can flow. With a suitably formed lower part of reactionchamber 1, a large proportion of the molten slag is captured on theinner walls of the chamber and is thereby separated from the gas.Because of the high density difference between the slag and the gas,molten slag droplets suspended in the gas can be separated by changingthe flow direction of the gas, e.g. by making the gas flow through arising channel 5, while the slag due to gravitation flows downwardsthrough a second passage 6, which leads to a slag dissolving vessel 14.Because there is an open passage between reaction chamber 1 and slagdissolving vessel 14, the pressures in these vessels are equal.

[0037] The gas and the molten slag are separated at a temperature notessentially different from the reaction temperature inside reactorchamber 1. The hot gas is led to a contact device 7, in which the gas israpidly cooled with a quench liquid. One embodiment of the presentinvention is that the quench liquid is sprayed into device 7 with anozzle 8. Inside the contact device 7 an intensive mixing of gas andquench liquid takes place, and the gas is quenched to a temperatureclose to the boiling point of water at the contact device pressure,which is nearly the same as the pressure in reactor chamber 1. The saltfumes that are contained in the hot gas are to a great extent capturedby the quench liquid. A part of the energy released when the gas isquenched will evaporate water from the quench liquid. This vapour ismixed with the gas that has been quenched.

[0038] The quench liquid is separated from the gas in device 9, fromwhich device the quench liquid is recirculated through nozzle 8 tocontact device 7. Makeup water is taken to the quench liquid loopthrough pipe 10. Optionally the pH of the quench liquid can be increasedby adding alkaline in the makeup water.

[0039] The molten slag flows through passage 6 down to pressure vessel14 to which water is led via piping 15. The liquid in vessel 14 isagitated, e.g., with an impeller 16 in vessel 14. The flow of incomingwater and its temperature are adjusted so that a certain amount of steamis released when the molten slag is dissolved in brine 11 in vessel 14.The steam flows up through passage 6 and prevents the hot gas fromentering vessel 14. This steam is mixed with the hot gas in channel 5.In this way the temperature in vessel 14 will not exceed the temperatureof the saturated steam released from brine 11. This makes the choice ofmaterial for pressure vessel 14 easier.

[0040] To stabilise the salt content and the volume of the liquid invessel 14, brine is extracted via piping 17. Some material contained bythe brine is not easily soluble. Usually the salt solution is alkaline,because part of the anionic organic matter is removed through oxidationand the corresponding cationic matter present in the slag has reactedwith carbon dioxide in the gas and formed carbonates. If this does nothappen, sodium carbonate or sodium sulphide, for example, can be broughtin with incoming water through piping 15. Heavy metals contained in theslag form practically insoluble carbonates and sulphides, a solidresidue. They can therefore be removed as a solid phase from the saltsolution. This is done with, e.g., a filter 18 or a centrifuge (notshown). If necessary, the brine can be cooled before the solid phase isseparated. The brine, from which the solid residue is removed, comes outas flow 19, while solid residue 20 is removed separately for furthertreatment.

[0041] The cooled exhaust gas flowing out from device 9 via piping 23consists mainly of carbon dioxide and water vapour. It also contains acertain amount of oxygen necessary to maintain an oxidising environmentin all parts of the equipment. The gas in duct 23 also contains acertain amount of droplets of concentrate, because the separation of thefinal concentrate from the cooled gas in device 9 may be incomplete.

[0042] The water vapour in the exhaust gas in duct 23 originates partlyfrom the residual moisture in the final concentrate that has been led toburner 3, partly from the reaction between oxygen and hydrogen presentin the organic matter of the final concentrate, and partly from pressurevessel 14. Also, the evaporation of quench liquid 8 in contact device 7increases the amount of water vapour in the exhaust gas.

[0043] By cooling the outgoing gas, most of the water vapour can becondensed and removed in liquid state. Droplets of entrained concentratein the condensate are also separated, which purifies the gas. At thesame time, the gas volume is substantially reduced. The condensation ofthe water content of the exhaust gas is illustrated in FIG. 1 by heatexchangers 21 and 22, to which the gas is led via piping 23. Cold wateris pumped via piping 15 through heat exchanger 21 and then via piping 24to heat exchanger 22, preferably in the countercurrent mode shown in theFigure. The water is heated and vaporised in the heat exchangers andexhausted as low-pressure steam through piping 25. The potentiallycontaminated condensate is discharged via piping 26. The quality of theconcentrate determines whether it can be used as process water orwhether it, e.g., should be combined with the waste liquor, from whichthe concentrate derives, and recirculated to the equipment describedherein.

[0044] The quenched gas is exhausted from heat exchanger 22 via piping27. Its main component is now carbon dioxide. It also contains thesurplus oxygen and possibly some traces of organic pollutants. The gasvolume is low because of the superatmospheric pressure and the lowtemperature after cooling. If required, the gas can still be led throughan adsorption device 28, for example, through a cartridge of activatedcarbon, before it is used as pure carbon dioxide elsewhere in theprocess or discharged into the atmosphere via a pressure relief valveand outlet 29.

[0045] The present invention will be further illustrated by thefollowing Example, which is intended to be illustrative in nature and isnot to be construed as limiting the scope of the invention.

EXAMPLE

[0046] A preferred embodiment of the present invention is described inthe following example. At the same time, the advantages of the inventionover known technology are pointed out.

[0047] A pulp mill with a daily production of 1,000 tons of bleachedsoftwood pulp can be considered typical for modern pulp industry. Themill uses chlorine dioxine and caustic soda as bleaching chemicals.During the bleaching process, approximately 20 kg of organic substancesare discharged per ton of pulp produced. Bleaching chemical residues, anadditional 20 kg of salts per ton of pulp, are also discharged. The saltis mostly sodium chloride. Part of the sodium is bound to organic acidsthat have been formed during the bleaching process. These substances aretransferred into the bleaching plant effluent. For this effluent achemical oxygen demand (COD) of 22 kg per ton of pulp is typical.

[0048] To achieve a complete oxidation of all organic matter—includingchlorinated organic matter—the oxidation must occur with a surplus ofoxygen at a temperature of about 1000° C. With the present inventionthis can be accomplished in the following way:

[0049] Feed liquor is expected to have reached a dry solids content ofabout 45% by means of evaporation. It is then preheated in devices 30and 31 to a temperature of 180° C.: The reaction chamber pressure is 10bar. At this temperature and dry solids content, half of which isoxidable organic material, the reaction temperature of 1000° C. can bemaintained in the reaction chamber, provided pure oxygen is used for thereaction. It is assumed that a surplus of 3 percent of oxygen is used inthe reactor.

[0050] In this case, 0.253 kg/s of oxygen 13 is brought to the reactorto achieve, in principle, complete oxidation. The reaction productsformed are 0.258 kg/s of inorganic molten slag and 1.090 kg/s of gas,consisting of carbon dioxide, water vapour and surplus oxygen. At atemperature of 1000° C. and with a superatmospheric pressure of 10 bar,the gas flow rate through the reactor outlet is 0.515 m³/s. With a gasvelocity of 10 m/s the flow cross section is 5.15 dm², corresponding toa pipe with an inner diameter of about 250 mm.

[0051] The flow of molten slag through reactor outlet 4 is about 0.215dm³/s. With a flow velocity of 1 m/s the molten slag fills a flow crosssection of about 0.02 dm³, which is below 1% of that of the gas. Thedensity of the gas in that state is about 2.11 kg/m³, while the densityof the flowing slag is about 1200 kg/m³. The separation of the moltenslag from the gas is therefore not difficult.

[0052] In case a salt concentration of about 35% is kept in thedissolving vessel 14, a flow of 0.92 kg/s of water has to be added viapiping 15. Of the water that has been added, about 0.17 kg/s isvaporised when the hot molten slag is quenched and dissolved in water.At an overpressure of 10 bar, the vapour reaches a temperature of about180° C. and the flow rate is 0.038 m³/s. If an inner diameter of 100 mmis chosen for passage 6, the steam upward flow velocity in the passageis about 5 m/s, which is sufficient to prevent hot gas from enteringvessel 14. If dissolving vessel 14 is designed for a residence time of1S minutes, the required brine volume is about 0.7 m³ in this vessel.

[0053] After direct evaporation in device 9, the exhaust gas to heatexchanger 21 contains about 0.355 kg/s of carbon dioxide, 0.0075 kg/s ofoxygen and 1,151 kg/s of water vapour. The total flow rate for the gasat an overpressure of 10 bar and temperature of 180° C. is 0.272 m³/s.If the chosen inner diameter for piping is 200 mm, the gas flow velocitywill be about 8.5 m/s. The vapour pressure in the gas is high, about 886kPa, which makes it possible to condense a substantial part of the watervapour from the withdrawn gas 23. If the gas is cooled to 100° C. in theheat exchanger 21, more than 98% of the vapour will condense, and thetotal exhaust gas flow becomes about 0.380 kg/s. Gas flow 23 at 10 barsuperatmospheric pressure is about 20 dm³/s, and can be transported in apipe with an inner diameter of 80 mm.

[0054] For comparison and to point out the advantages of the inventionover the state-of-the-art technology, the same calculation is performedfor the case where evaporated effluent from the same assumed bleachplant is incinerated in the conventional way.

[0055] With conventional technology, the concentrate would be disposedof in an atmospheric incinerator with air as the source of oxygen. It islikely that the waste liquor would be evaporated to a dry solids contenthigher than 45%, which, as described in the above example, would besufficient according to the present invention. Let us assume that theconcentrate is evaporated to a dry solids content of 50% before it isfed into the incinerator.

[0056] To reach a combustion temperature of 1000° C., supplementary fuelis needed in the incinerator. Because of the nitrogen ballast in thecombustion air, about 0.6 kg of oil is needed for each kilogram of drysolids of concentrate. Because the gases are of atmospheric pressure,water vapour can not be condensed from the exhaust gas at temperaturesabove 100° C. and thus cannot be used for production of pressurisedsteam. Provided no large quantities of low-grade warm water areproduced, the water vapour is exhausted with the gases, which has beenassumed when calculating the values in the table below.

[0057] The following Table gives data for comparison of concentrateoxidation as accomplished with the present invention and as performedwith the state-of-the-art technology. The figures refer to the pulp millbleach plant example given previously.

[0058] Comparison between the invention and state-of-the-art technologyState-of- Invention the-art Feed dry solids content % 45.0 50.0 Oxygenconsumption kg/h 912 — Oil consumption kg/h — 995 Reactor temperature °C. 1000 1000 Residence time in reactor s 2 2 Reactor volume m³ 1.0 23.2Exhaust gas temperature ° C. 100 100 Discharged exhaust gas volume m³/h72 25,400

[0059] As can be seen, the present invention makes it possible tooxidise the concentrate at the required 1000° C. reactor temperaturewith a lower dry solids content of the feed concentrate. In this exampleof the invention, the oxidation is done with pure oxygen. Also, thenovel procedure does not require any supplementary fuel, contrary toconventional methods. The amounts of oxygen in the novel technology andfuel oil in the state-of-the-art technology are nearly equal.

[0060] As the cost of oxygen per kg is about half the cost of fuel oilper kg, the operating costs of the novel technology will be considerablysmaller than those of conventional methods.

[0061] The present invention leads to a significantly smaller equipmentvolume as can be seen in the comparison between the required reactorvolumes. According to the present invention, the reactor volume is lessthan 5% of the combustion chamber volume in conventional incineratorswith corresponding design values. The difference between the exhaust gasvolumes is notable, too. This is reflected in the size and cost of theequipment for transporting and cleaning of the exhaust gas.

1 1 1 10 PRT Homo sapiens 1 Glu His Trp Ser Tyr Gly Leu Arg Pro Gly 1 510

We claim:
 1. An LHRH antagonist comprising a peptide compound, wherein aresidue of the peptide compound corresponding to the amino acid atposition 6 of natural mammalian LHRH comprises D-Lys(Imdac),D-Lys(Ppic), D-Lys(Dodac), D-Lys(pGlu), D-Lys(Otac) and D-Lys(Onic) or amoiety selected from the group consisting of a dipolar moiety, asulfonium moiety, a receptor-modifying moiety and a small polar moiety,such that the peptide compound has LHRH antagonist activity, with theprovisos that the dipolar moiety is not a zwitterionic pyridinium andthe residue is not D-Cit, D-Hci or a lower alkyl derivative of D-Cit orD-Hci.
 2. The LHRH antagonist of claim 1, wherein the peptide compoundcomprises about 8 to about 12 residues.
 3. The LHRH antagonist of claim1, wherein the peptide compound comprises 10 residues.
 4. A peptidecompound comprising a structure: A-B-C-D-E-F-G-H-I-J wherein A ispyro-Glu, Ac-D-Nal , Ac-D-Qal, Ac-Sar, or Ac-D-Pal; B is His or4-CI-D-Phe; C is Trp, D-Pal. D-Nal, L-Nal, D-Pal(N-O), or D-Trp; D isSer; E is N-Me-Ala, Tyr, N-Me-Tyr, Ser, Lys(iPr), 4-Cl-Phe, His, Asn,Met, Ala, Arg or lie; F is D-Lys(Imdac), D-Lys(Ppic), D-Lys(Dodac),D-Lys(pGlu), D-Lys(Otac), D-Lys(Onic) or a structure:

wherein R and X are independently, H or alkyl; and Y comprises a moietyselected from the group consisting a dipolar moiety, a sulfonium moiety,a receptor-modifying moiety and a small polar moiety, the provisos thatthe dipolar moiety- is not a zwinerionic pyridinium and F is not D-Cit,D-Hci or a lower alkyl derivative of D-Cit or D-Hci; G is Leu or Trp; His Lys(iPr), Gln, Met, or Arg; I is Pro; and J is Gly-NH₂ or D-Ala-NH₂;or a pharmaceutically acceptable salt thereof.
 5. The peptide compoundof claim 4, wherein Y comprises a dipolar moiety, with the proviso thatthe dipolar moiety is not a zwitterionic pyridinium.
 6. The peptidecompound of claim 5, wherein Y comprises a moiety selected from thegroup consisting of ylids, tertiary amine oxides, nitrile oxides andpyridine-N-oxides.
 7. The peptide compound of claim 4, wherein Ycomprises a sulfonium moiety.
 8. The peptide compound of claim 4,wherein Y comprises a receptor-modifying moiety.
 9. The peptide compoundof claim 8, wherein Y comprises a moiety selected from the groupconsisting of ylids, sulfonium moieties, a-halocarbonyls, sulfates,sulfonates, alkyl halides and benzyl halides.
 10. The peptide compoundof claim 9, wherein Y comprises an α-halocarbonyl.
 11. The peptidecompound of claim 4, wherein F is D-Lys(lmdac), D-Lys(Ppic) andD-Lys(Dodac), D-Lys(pGlu), D-Lys(Otac) or D-Lys(Onic).
 12. The peptidecompound of claim 2, wherein Y comprises a small polar moiety, with theproviso that F is not D-Cit, D-Hci or a lower alkyl derivative of D-Citor D-Hci.
 13. The peptide compound of claim 12, wherein F is selectedfrom the group consisting of D-Asn, D-Gln and D-Thr.
 14. An LHRHantagonist comprising a peptide compound, wherein a residue of thepeptide compound corresponding to the amino acid at position 6 ofnatural mammalian LHRH comprises a small polar moiety such that thepeptide compound has LHRH antagonist activity, with the proviso that theresidue is not D-Cit, D-Hci or a lower alkyl derivative of D-Cit orD-Hci.
 15. The LHRH antagonist of claim 14, wherein the antagonist hasan antiovulatory activity of less than about 1 μg per rat in a ratantiovulation assay.
 16. The LHRH antagonist of claim 14, wherein theantagonist has an ED₅₀ in a histamine release assay of at least about 5μg/ml.
 17. The LHRH antagonist of claim 14, wherein the peptide compoundcomprises about 8 to about 12 residues.
 18. The LHRH antagonist of claim14, wherein the peptide compound comprises 10 residues.
 19. A peptidecompound comprising a structure: A-B-C-D-E-F-G-H-I-J wherein A ispyro-Glu, Ac-D-Nal , Ac-D-Qal, Ac-Sar, or Ac-D-Pal B is His or4-Cl-D-Phe C is Trp, D-Pal, D-Nal, L-Nal, D-Pal(N-0), or D-Trp D is SerE is N-Me-Ala, Tyr, N-Me-Tyr, Ser, Lys(iPr), 4-Cl-Phe, His, Asn, Met,Ala, Arg or Ile; F is

wherein R and X are, independently, H or alkyl; and L comprises a smallpolar moiety, with the proviso that F is not D-Cit, D-Hci or a loweralkyl derivative of D-Cit or D-Hci; G is Leu or Trp; H is Lys(iPr), Gin,Met, or Arg I is Pro; and J is Gly-NH₂ or D-Ala-NH₂; or apharmaceutically acceptable salt thereof.
 20. The peptide compound ofclaim 19, wherein F is selected from the group consisting of D-Asn,D-Gin and D-Thr.
 21. A peptide compound comprising a structure:A-B-C-D-E-F-G-H-I-J wherein A is pyro-Glu, Ac-D-Nal, Ac-D-Qal, Ac-Sar,or Ac-D-Pal; B is His or 4-Cl-D-Phe; C is Trp, D-Pal, D-Nal, L-Nal,D-Pal(N-O), or D-Trp; D is Ser; E is N-Me-Ala, Tyr, N-Me-Tyr, Ser,Lys(iPr), 4-Cl-Phe, His, Asn, Met, Ala, Arg or Ile; F is D-Asn; G is Leuor Trp; H is Lys(iPr), Gln, Met, or Arg; I is Pro; and J is Gly-NH₂ orD-Ala-NH₂; or a pharmaceutically acceptable salt thereof.
 22. A peptidecompound comprising a structure: A-B-C-D-E-F-G-H-I-J wherein A ispyro-Glu, Ac-D-Nal , Ac-D-Qal, Ac-Sar, or Ac-D-Pal; B is His or4-Cl-D-Phe; C is Trp, D-Pal, D-Nal, L-Nal, D-Pal(N—O), or D-Trp; D isSer; E is N-Me-Ala, Tyr, N-Me-Tyr, Ser, Lys(iPr), 4-Cl-Phe, His, Asn,Met, Ala, Arg or Ile; F is D-Arg, D-Lys(iPr), D-Pal(iPr), D-Cit or Q,wherein Q has a structure

wherein R and X are, independently, H or alkyl; and Z comprises asulfonium moiety; G is Leu or Trp; H is Lys(iPr), Gln, Met, Arg or Q; Iis Pro; and J is Gly-NH₂ or D-Ala-NH₂; with the proviso that at leastone of F and H is Q; or a pharmaceutically acceptable salt thereof. 23.A peptide compound comprising a structure:Ac-D-Nal4-Cl-Phe-D-Pal-Ser-Tyr-D-Pal(N—O)-Leu-Lys(iPr)-Pro-D-Ala-NH₂. ora pharmaceutically acceptable salt thereof.
 24. A peptide compoundcomprising a structureAc-D-Nal4-Cl-D-Phe-D-Pal-Ser-Tyr-D-Pal(CH₂COO⁻)-Leu-Lys(iPr)-Pro-D-Ala-NH₂;or a pharmaceutically acceptable salt thereof.
 25. A peptide compoundcomprising a structureAc-Sar-4-Cl-D-Phe-D-Nal-Ser-Tyr-D-Pal(Bzl)-Leu-Lys(iPr)-Pro-D-Ala-NH₂;or a pharmaceutically acceptable salt thereof.
 26. A peptide compoundcomprising a structure:Ac-D-Nal4-Cl-D-Phe-D-Trp-Ser-Tyr-D-Met(S⁺Me)-Leu-Arg-Pro-D-Ala-NH₂; or apharmaceutically acceptable salt thereof.
 27. A peptide compoundcomprising a structure:Ac-D-Nal-4-Cl-D-Phe-D-Pal-Ser-Tyr-D-Arg-Leu-Met(S⁺Me)-Pro-D-Ala-NH₂; ora pharmaceutically acceptable salt thereof.
 28. A peptide compoundcomprising a structure:Ac-D-Nal-4-Cl-D-Phe-D-Pal-Ser-Tyr-D-Lys(Imdac)-Leu-Lys(iPr)-Pro-D-Ala-NH₂;or a pharmaceutically acceptable salt thereof.
 29. A peptide compoundcomprising a structure:Ac-D-Nal-4-Cl-D-Phe-D-Pal-Ser-N-Me-Tyr-D-Asn-Leu-Lys(iPr)-Pro-D-Ala-NH₂;or a pharmaceutically acceptable salt thereof.
 30. A peptide compoundcomprising a structure:Ac-D-Nal4-Cl-D-Phe-D-Pal-Ser-Tyr-D-Asn-Leu-Lys(iPr)-Pro-D-Ala-NH₂; or apharmaceutically acceptable salt thereof.
 31. A peptide compoundcomprising a structure selected from the group consisting of:Ac-D-Nal¹,4-Cl-D-Phe², D-Pal³, D-Gln⁶-Lys(iPr)⁸, D-Ala¹⁰-LHRH Ac-D-Nal¹,4-Cl-D-Phe², D-Pal³, D-Asn⁶-Lys(iPr)⁸, D-Ala¹⁰-LHRH Ac-D-Nal¹.4-Cl-D-Phe², D-Pal³, D-Thr⁶-Lys(iPr)⁸, D-Ala¹⁰-LHRH Ac-D-Nal¹,4-Cl-D-Phe², D-Pal³, D-Cit⁶-Lys(iPr)⁸, Pip⁹-D-Ala¹⁰-LHRH Ac-D-Nal¹,4-Cl-D-Phe², D-Pal³, D-Glu(Taurine)⁶-Lys(iPr)⁸, D-Ala¹⁰-LHRH Ac-D-Nal¹,4-Cl-D-Phe², D-Pal³, D-Cit⁶-Lys(iPr)⁸-LHRH Ac-D-Nal¹, 4-Cl-D-Phe²,D-Pal³, D-Cit⁶-Lys(iPr)⁸, Pip⁹-LHRH Ac-D-Nal¹,4-Cl-D-Phe², D-Pal³,D-Phe(4-NO₂)⁶-Lys(iPr)⁸, D-Ala¹⁰-LHRH Ac-D-Nal¹, 4-Cl-D-Phe², D-Pal³,D-Cit⁶-Lys(iPr)⁸, ProNHEt⁹-des-Gly¹⁰-LHRH Ac-D-(or L)-9-anthryl-Alal,4-Cl-D-Phe², D-Pal³, D-Cit⁶-Lys(iPr)⁸, D-Ala¹⁰-LHRH Ac-L-(orD)-9-anthryl-Ala¹, 4-Cl-D-Phe², D-Pal³, D-Cit⁶-Lys(iPr)⁸, D-Ala¹⁰-LHRHAc-D-(or L)-Ada-Ala¹, 4-Cl-D-Phe², D-Pal³, D-Cit⁶-Lys(iPr)⁸,D-Ala¹⁰-LHRH Ac-L-(or D)-Ada-Ala¹, 4-Cl-D-Phe², D-Pal³,D-Cit⁶-Lys(iPr)⁸, D-Ala¹⁰-LHRH Ac-D-Nal¹, 4-Cl-D-Phe², D-Pal³,D-Lys(Glc)⁶-Lys(iPr)⁸, D-Ala¹⁰-LHRH Ac-D-Nal¹, 4-Cl-D-Phe², D-Pal³,D-Pal(1-Bu)⁶, Lys(iPr)⁸, D-Ala¹⁰-LHRH Ac-D-Nal¹, 4-Cl-D-Phe2, D-Pal³,D-Pal(Bzl)⁶, Lys(iPr)⁸, D-Ala¹⁰-LHRH Ac-D-Nal¹, 4-Cl-D-Phe², D-Pal³,Pal⁵, D-Pal(ipr)⁶, Lys(iPr)⁸, D-Ala¹⁰-LHRH Ac-D-Nal¹, 4-Cl-D-Phe²,D-Pal³, Cit⁵, D-Cit⁶, Lys(iPr)⁸, D-Ala¹⁰-LHRH Ac-D-Nal¹, 4-Cl-D-Phe²,D-Pal³, Pal³, D-Cit⁶, Lys(iPr)⁸, D-Ala¹⁰-LHRH Ac-D-Nal¹, 4-Cl-D-Phe²,D-Pal³, Cit⁵, D-Pal⁶, Lys(iPr)⁸, D-Ala¹⁰-LHRH Ac-D-Nal¹, 4-Cl-D-Phe²,D-Pal³, Asn⁴, Tyr⁵, D-Cit⁶, Lys(iPr)⁸, D-Ala¹⁰-LHRH Ac-D-Nal¹,4-Cl-D-Phe², D-Pal³, Cit⁵, D-Pal(iPr)⁶, Lys(iPr)⁸, D-Ala¹⁰-LHRHAc-D-Nal¹, 4-Cl-D-Phe², D-Pal³, D-HomoArg(NO₂)⁶, Lys(iPr)⁸, D-Ala¹⁰-LHRHAc-D-Nal¹, 4-Cl-D-Phe², D-Pal³, D-Lys(Glycolyl)⁶, Lys(iPr)⁸,D-Ala¹⁰-LHRH Ac-D-Nal¹, 4-Cl-D-Phe², D-Pal³, D-Lys(iPrPic)⁶, Lys(iPr)⁸,D-Ala¹⁰-LHRH Ac-D-Nal¹, 4-Cl-D-Phe², D-Pal³, D-Lys(HomoPro)⁶, Lys(iPr)⁸,D-Ala¹⁰-LHRH Ac-D-Nal¹, 4-Cl-D-Phe², D-Pal³, D-Pal(iPr)⁶, Lys(iPr)⁸,D-Ala¹⁰-LHRH Ac-D-Nal¹, 4-Cl-D-Phe², D-Pal³, D-Lys(3-pyridineacetic)⁶,Lys(iPr)⁸, D-Ala¹⁰-LHRH Ac-D-Nal¹, 4-Cl-D-Phe², D-Pal³, D-Lys(2-ClNic)⁶,Lys(iPr)⁸, D-Ala¹⁰-LHRH Ac-N^(α)Me-D-Nal¹, 4-Cl-D-Phe², D-Pal³, D-Cit⁶,Lys(iPr)⁸, D-Ala¹⁰-LHRH Ac-D-Nal¹, 4-Cl-D-Phe², D-Pal³, Lys(Otac)⁵,D-Lys(Otac)⁶, Lys(iPr)⁸, D-Ala¹⁰-LHRH Ac-D-Nal¹, 4-Cl-D-Phe2, D-Pal³,Lys(ONic)⁵, D-Lys(ONic)⁶, Lys(iPr)⁸, D-Ala¹⁰-LHRH Ac-D-Nal¹,4-Cl-D-Phe², D-Pal³, Lys(Pyz)⁵,D-Lys(Pyz)⁶, Lys(iPr)⁸, D-Ala¹⁰-LHRHAc-D-Nal¹, 4-Cl-D-Phe², D-Pal³, D-GLu⁶ Lys(iPr)⁸, D-Ala¹⁰-LHRHAc-D-Nal¹, 4-Cl-D-Phe², D-Pal³, D-Lys⁶, Lys(iPr)⁸, D-Ala¹⁰-LHRHAc-D-Nal¹, 4-Cl-D-Phe², D-Pal³, D-Lys(Gulonyl)⁶, Lys(iPr)⁸, D-Ala¹⁰-LHRHAc-D-Nal¹, 4-Cl-D-Phe2, D-Pal³, D-Lys(iPrNic)⁵, D-Lys(iPrNic)⁶,Lys(iPr)8, D-Ala¹⁰-LHRH Ac-D-Nal¹, 4-Cl-D-Phe², D-Pal³, D-Lys(ONic)⁶,Lys(iPr)⁸, D-Ala¹⁰-LHRH Ac-D-Nal ¹, 4-Cl-D-Phe², D-Pal³, D-Lys(OTac)⁶,Lys(iPr)⁸, D-Ala¹⁰-LHRH Ac-D-Nal¹, 4-Cl-D-Phe², D-Pal³, D-Lys(Pyz)⁶,Lys(iPr)⁸, D-Ala¹⁰-LHRH Ac-D-Nal¹, 4-Cl-D-Phe², D-Pal³, D-Lys(nBuNic)⁶,Lys(iPr)⁸, D-Ala¹⁰-LHRH Ac-D-Nal¹, 4-Cl-D-Phe², D-Pal³, D-Glu(Amp)⁶,Lys(iPr)⁸, D-Ala¹⁰-LHRH Ac-D-Nal¹, 4-Cl-D-Phe², D-Pal³, D-Glu(Dea)⁶,Lys(iPr)⁸, D-Alal¹⁰-LHRH Ac-D-Nal¹, 4-Cl-D-Phe², D-Pal³, Lys(pGlu)⁵,D-Lys(pGlu)⁶, Lys(iPr)⁸, D-Ala¹⁰-LHRH Ac-D-Nal¹, 4-Cl-D-Phe², D-Pal³,N^(α)Me-Tyr⁵, D-Pal(iPr)⁶, Lys(iPr)⁸, D-Ala¹⁰-LHRH Ac-D-Nal¹,C^(α)Me-4Cl-Phe², D-Pal³, N^(α)Me-Tyr⁵, D-Pal(ipr)⁶, Lys(iPr)⁸,D-Ala¹⁰-LHRH Ac-D-Nal¹, 4-Cl-D-Phe², D-Pal3, Lys(CNa)⁶, Lys(iPr)⁸,D-Ala¹⁰-LHRH Ac-D-Nal¹, 4-Cl-D-Phe², D-Pal³, D-GLu(PEG)⁶, Lys(iPr)⁸,D-Ala¹⁰-LHRH Ac-D-Nal¹, 4-Cl-D-Phe², D-Pal³, D-Lys(Oxa)⁶, Lys(iPr)⁸,D-Ala¹⁰-LHRH Ac-D-Nal¹, 4-Cl-D-Phe², D-Pal³, Lys(CNa)⁵, D-Lys(CNa)⁶,Lys(iPr)⁸, D-Ala¹⁰-LHRH Ac-D-Nal¹, 4-Cl-D-Phe², D-Pal³, Lys(ClNic)⁵,D-Lys(ClNic)⁶, Lys(iPr)⁸, D-Ala¹⁰-LHRH Ac-D-Nal¹, 4-Cl-D-Phe², D-Pal³,D-Lys(Ac)⁶, Lys(iPr)⁸, D-Ala¹⁰-LHRH Ac-D-Nal¹, 4-Cl-D-Phe², D-Pal³,D-Glu(Tris)⁶, Lys(ipr)⁸, D-Ala¹⁰-LHRH Ac-D-Nal¹, 4-Cl-D-Phe2, D-Pal³,D-Gln(iPr)⁶, Lys(iPr)⁸, D-Ala¹⁰-LHRH Ac-D-Nal¹, 4-Cl-D-Phe², D-Pal³,D-Glu(CSer)⁶, Lys(ipr)⁸, D-Ala¹⁰-LHRH Ac-D-Nal¹, 4-Cl-D-Phe², D-Pal³,D-Glu(Mop)⁶, Lys(iPr)⁸, D-Ala¹⁰-LHRH Ac-D-Nal¹, 4-Cl-D-Phe², D-Pal³,Lys⁵, D-Pal(iPr)⁶, Lys(iPr)⁸, D-Ala¹⁰-LHRH Ac-D-Nal¹, 4-Cl-D-Phe²,D-Pal³, Lys(Nic)⁵, D-Pal(iPr)⁶, Lys(iPr)⁸, D-Ala¹⁰-LHRH Ac-D-Nal¹,4-Cl-D-Phe2, D-Pal³, Lys(Ac)⁵, D-Pal(iPr)⁶, Lys(iPr)⁸, D-Ala¹⁰-LHRHAc-D-Nal¹, 4-Cl-D-Phe², D-Pal³, D-Glu(DEGA)⁶, Lys(iPr)⁸, D-Ala¹⁰-LHRHAc-D-Nal¹, 4-Cl-D-Phe². D-Pal³, Lys(Nic)⁵, D-Pal(Bzl)⁶, Lys(iPr)⁸,D-Ala¹⁰-LHRH Ac-D-Nal¹, 4-CI-D-Phe², D-Pal³, Lys(Ac)⁵, D-Pal(Bzl)⁶,Lys(ipr)⁸, D-Ala¹⁰-LHRH Ac-D-Nall, 4-Cl-D-Phe², D-Pal³, Lys(TFAc)⁶,Lys(iPr)⁸, D-Ala¹⁰-LHRH Ac-D-Nal¹, 4-Cl-D-Phe², D-Pal³, Lys⁵,D-Pal(Bzl)⁶, Lys(iPr)⁸, D-Ala¹⁰-LHRH Ac-D-Nal¹, 4-Cl-D-Phe², D-Pal³,Lys(iPr)⁵, D-Lys(Nic)⁶, Lys(iPr)⁸, D-Ala¹⁰-LHRH Ac-D-Nal¹, 4-Cl-D-Phe²,D-Pal³, Lys(iPr)⁵, D-Lys(Pic)⁶, Lys(iPr)⁸, D-Ala¹⁰-LHRH Ac-D-Nal¹,4-Cl-D-Phe², D-Pal³, Lys(TFAc)⁵, D-Lys(TFAc)⁶, Lys(iPr)⁸, D-Ala¹⁰-LHRHAc-D-Nal¹, 4-Cl-D-Phe², D-Pal³, Lys(iPr)⁵, 4-Cl-D-Phe⁶, Lys(iPr)⁸,D-Ala¹⁰-LHRH Ac-D-Nal¹, 4-Cl-D-Phe², D-Pal³, Lys(iPr)⁵, D-Nal⁶,Lys(iPr)⁸, D-Ala¹⁰-LHRH Ac-D-Nal¹, 4-Cl-D-Phe², D-Pal³, Lys(iPr)⁵,D-Lys(pGlu)⁶, Lys(iPr)⁸, D-Ala¹⁰-LHRH Ac-D-Nal¹, 4-Cl-D-Phe², D-Pal³,Lys(iPr)⁵, D-Lys(OTac)⁶, Lys(iPr)⁸, D-Ala¹⁰-LHRH Ac-D-Nal¹. 4-Cl-D-Phe²,D-Pal³, Ile⁵, D-Pal(Bzl)⁶, Lys(iPr)⁸, D-Ala¹⁰-LHRH Ac-D-Nal¹,4-Cl-D-Phe², D-Pal³, Lys(Pic)⁵, D-Pal(iPr)⁶, Lys(iPr)⁸, D-Ala¹⁰-LHRHAc-D-Nal¹, 4-Cl-D-Phe², D-Pal³, D-Lys(3-Δ-Pro)⁶, Lys(iPr)⁸,D-Ala¹⁰-LHRH-TFAAc-D-Nal-4-Cl-D-Phe2,D-Pal³,D-Lys(Ac-D-Nal¹,4-Cl-D-Phe2,D-Pal³,Ser)⁶,Lys(iPr)⁸,D-Ala¹⁰-LHRHAc-D-Qal¹,4-Cl-D-Phe²,D-Pal³,D-Lys(pGlu)⁶, Lys(iPr)⁸,D-Ala¹⁰-LHRHAc-D-Qal¹, 4-Cl-D-Phe²,D-Pal³,D-Lys(Ac)⁶, Lys(iPr)⁸,D-Ala¹⁰-LHRHAc-D-Nal¹,4-Cl-D-Phe²,D-Pal³,D-Lys(lmdac)⁶, Lys(iPr)⁸,D-Ala¹⁰-LHRHAc-D-Qal¹, 4-Cl-D-Phe²,D-Pal³,D-Lys(Dodac)⁶, Lys(iPr)⁸,D-Ala¹⁰-LHRHAc-D-Nal¹, 4-Cl-D-Phe²,D-Pal³,Ser⁵,D-Pal(iPr)⁶,Lys(iPr)⁸,D-Ala¹⁰-LHRHAc-D-Nal¹,4-Cl-D-Phe²,D-Pal³,D-Lys(iPr)⁵, D-Lys(TFAC)⁶,Lys(iPr)⁸,D-Ala¹⁰-LHRH Ac-D-Nal¹,4-Cl-D-Phe²,D-Pal³,His⁵D-Pal(iPr)⁶, Lys(iPr)⁸,D-Ala¹⁰-LHRHAc-D-Nal¹,4-Cl-D-Phe²,D-Pal³,Asn⁵,D-Pal(iPr)⁶, Lys(iPr)⁸,D-Ala¹⁰-LHRHAc-D-Nal¹,4-Cl-D-Phe2,D-Pal³,Lys(iPr)⁵,D-Lys(4HBc)⁶,Lys(iPr)⁸,D-Ala10-LHRHAc-D-Nal¹,4-Cl-D-Phe²,D-Pal³,Met⁵,D-Pal(iPr)⁶, Lys(iPr)⁸,D-Ala¹⁰-LHRHAc-D-Nal¹,4-Cl-D-Phe²,D-Phe²,D-Pal³,Ala⁵,D-Pal(iPr)⁶,Lys(iPr)⁸,D-Ala¹⁰-LHRHAc-D-Nal¹,4-Cl-D-Phe²,D-Pal³,N-Me-Ala⁵,D-Pal(iPr)⁶,Lys(iPr)⁸,D-Ala¹⁰-LHRHAc-D-Nal¹,4-Cl-D-Phe²,D-Pal³,D-Lys(Hippic)⁶, Lys(iPr)⁸,D-Ala¹⁰-LHRHAc-D-Nal¹,4-Cl-D-Phe2,D-Pal³,D-Lys(AcGly)⁶, Lys(iPr)⁸,D-Ala¹⁰-LHRHAc-D-Nal¹,4-Cl-D-Phe²,D-Pal³,D-Lys(ppic)⁶, Lys(iPr)⁸,D-Ala¹⁰-LHRHAc-D-Nal¹,4-Cl-D-Phe2,D-Pal³,D-Lys(Mts)⁶, Lys(ipr)⁸,D-Ala¹⁰-LHRHAc-D-Nal¹,4-Cl-D-Phe²,D-Pal³,D-Lys(Orotic)⁶, Lys(iPr)⁸,D-Ala¹⁰-LHRHAc-Sar¹, 4-Cl-D-Phe²,D-Nal³,D-Pal(Bzl)⁶, Lys(iPr)⁸,D-Ala¹⁰-LHRHAc-Sar¹,4-Cl-D-Phe², 1-1-Nal³,D-Pal(Bzl)⁶, Lys(iPr)⁸,D-Ala¹⁰-LHRHAc-D-Nal¹, 4-Cl-D-Phe²,D-Pal³,D-Pal(CH₂COOH)⁶,Lys(iPr)⁸,D-Ala¹⁰-LHRHAc-D-Nal¹, 4-Cl-D-Phe²,D-Pal³,D-Lys(Ala)⁶, Lys(iPr)⁸,D-Ala¹⁰-LHRHAc-Sar¹,4-Cl-D-Phe²,D-1-Nal³,D-Pal(iPr)⁶, Lys(iPr)⁸,D-Ala¹⁰-LHRHAc-Sar¹, 4-Cl-D-Phe²,L-1-Nal³,D-Pal(iPr)⁶, Lys(ipr)⁸,D-Ala¹⁰-LHRHAc-D-Qa¹,4-Cl-D-Phe²,D-Pal³,D-Lys(Gulonyl)⁶,Lys(iPr)⁸,D-Ala¹⁰-LHRHAc-D-Na¹,4-Cl-D-Phe²,D-Pal³,D-Pal(N—O)⁶, Lys(iPr)⁸,D-Ala¹⁰-LHRHAc-D-Qal¹, 4-Cl-D-Phe²,D-Pal³,D-Lys(Ppic)⁶, Lys(iPr)⁸,D-Ala¹⁰-LHRHAc-D-Qal¹, 4-Cl-D-Phe²,D-Pal³,D-Lys(Imdac)⁶, Lys(iPr)⁸,D-Ala¹⁰-LHRHAc-D-Qal¹, 4-Cl-D-Phe²,D-Pal³,D-Lys(Onic)⁶, Lys(iPr)⁸,D-Ala¹⁰-LHRHAc-D-Qal¹, 4-Cl-D-Phe²,D-Pal³,D-Lys(Otac)⁶, Lys(iPr)⁸,D-Ala¹⁰-LHRHAc-D-Nal¹, 4-Cl-D-Phe²,D-Pal³,D-Lys(Dodac)⁶, Lys(iPr)⁸,D-Ala¹⁰-LHRHAc-D-Pal¹, 4-Cl-D-Phe²,D-Pal³,D-Pal(iPr)⁶, Lys(iPr)⁸,D-Ala¹⁰-LHRHAc-D-Nal¹, 4-Cl-D-Phe²,D-Pal³,N-Me-Tyr⁵,D- Asn⁶,Lys(iPr)⁸,D-Ala¹⁰-LHRHAc-D-Nal¹,4-Cl-D-Phe²,D-Pal³,N-Me-Tyr⁵,D-Lys(Onic)⁸,Lys(iPr)⁸,D-Ala10-LHRHAc-D-Nal¹,4-Cl-D-Phe²,D-Pal³,N-Me-Tyr⁵,D-Lys(Ac)⁶,Lys(iPr)⁸,D-Ala¹⁰-LHRHAc-D-Nal¹, 4-Cl-D-Phe²,D-Pal³,Lys(iPr)⁵,D-His⁶,Trp⁷, Orn⁸,D-Ala¹⁰-LHRHAc-D-Nal¹, 4-Cl-D-Phe²,D-Pal³,His⁵,D-Arg⁶, Trp⁷,Orn⁸,D-Ala¹⁰-LHRHAc-D-Nal¹, 4-Cl-D-Phe²,D-Pal³,Arg⁵,D-His⁶, Trp⁷,Orn8,D-Ala¹⁰-LHRHAc-D-Nal¹, 4-Cl-D-Phe²,D-Pal³,Lys(iPr)⁵,D-Trp⁶,Trp⁷, Orn⁸,D-Ala¹⁰-LHRHAc-D-Nal¹, 4-Cl-D-Phe²,D-Pal³, 4-Cl-Phe⁵,D-Pal(iPr)⁶,Lys(iPr)⁸,D-Ala¹⁰-LHRH Ac-D-Nal¹,4-Cl-D-Phe²,D-Pal(N—O)³,D-Pal(iPr)⁶,Lys(iPr)⁸,D-Ala¹⁰-LHRH Ac-D-Nal¹,4-Cl-D-Phe²,D-Trp³,D-Arg⁶, Met⁸,D-Ala¹⁰-LHRH Ac-D-Nal¹,4-Cl-D-Phe²,D-Trp³,D-Arg⁶, Met(S⁺Me)⁸,D-Ala¹⁰-LHRH Ac-D-Nal¹,4-Cl-D-Phe²,D-Trp³,D-Met⁶,D-Ala¹⁰-LHRH Ac-D-Nal¹,4-Cl-D-Phe²,D-Trp³,D-Met(S⁺Me)⁶, D-Ala¹⁰-LHRH Ac-D-Nal¹,4-Cl-D-Phe²,D-Trp³,D-Arg⁶, Lys(COCH₂Br)⁸,D-Ala¹⁰-LHRH Ac-D-Nal¹,4-Cl-D-Phe²,D-Trp³,D-Met(S⁺Me)⁶, Met(S⁺Me)⁸,D-Ala¹⁰-LHRH Met(S⁺Me)⁸-LHRHLys(COCH₂Br)⁸-LHRH Ac-D-Nal¹,4-Cl-D-Phe²,D-Trp³,D-Lys(COCH₂Br)⁶,D-Ala¹⁰-LHRH Ac-D-Nal¹,4-Cl-D-Phe²,D-Pal³,D-Lys(COCH₂CH₂N(Et)₂)⁶ D-Ala¹⁰-LHRH Ac-D-Na¹,4-Cl-D-Phe²,D-Pal³,D-Lys(2-pyrimidylthio)acetic)⁶,Lys(iPr)⁸,D-Ala¹⁰-LHRH Ac-D-Nal¹, 4-Cl-D-Phe²,D-Trp³,D-Met(S⁺CH₂C H₅)⁶,D-Ala¹⁰-LHRHAc-D-Na¹, 4-Cl-D-Phe²,D-Pal³, D-Met(S⁺CH₃),D-Ala¹⁰-LHRH Ac-D-Nal¹,4-Cl-D-Phe²,D-Pal³,D-Met(S+CH₂COPh)⁶,D-Ala¹⁰-LHRH Ac-D-Na¹,4-Cl-D-Phe²,D-Pal³,D-Dap(COCH2S⁺Me₂)⁶,D-Ala¹⁰-LHRH Ac-D-Nal¹,4-Cl-D-Phe²,D-pal³His⁵D-Pal(iPr)⁶, Lys(ipr)⁸,D-Ala¹⁰-LHRH Ac-D-Na¹,4-Cl-D-Phe²,D-Pal³, D-Arg⁶, Met(S+Me)⁸,D-Ala¹⁰-LHRH Ac-D-Nal¹,4-Cl-D-Phe²,D-Trp³,D-Met(S⁺CH₂—CH═CH₂)⁶,D-Ala¹⁰-LHRH Ac-D-Na¹,4-Cl-D-Phe²,D-Pal³,D-Arg⁶, Orn(COCH₂S⁺Me₂)⁸,D-Ala¹⁰,LHRH Ac-D-Nal¹,4-Cl-D-Phe²,D-Pal³,D-Arg⁶, Orn(COCH₂SMe)⁸,D-Ala¹⁰-LHRHAc-D-Nal¹.4-Cl-D-Phe²,D-Pal³,D-Arg⁶,Met 8, D-Ala¹⁰-LHRH Ac-D-Na¹,4-Cl-D-Phe²,D-Pal³,D-Lys(COCH₂S⁺Me²)⁶,D-Ala¹⁰-LHRH Ac-D-Nal¹,4-Cl-D-Phe²,D-Pal³,D-Arg⁶, Lys(COCH₂S⁺Me₂)⁸,D-Ala¹⁰-LHRH Ac-D-Nal¹,4-Cl-D-Phe²,D-Pal³,D-Met(S⁺Me)⁶, Met(S⁺Me)⁸,D-Ala¹⁰-LHRHAc-D-Nal¹,4-Cl-D-Phe²,D-Pal³,D-Orn(COCH⁻)S⁺Me²)⁶,D-Ala¹⁰-LHRH Ac-D-Na¹,4-Cl-D-Phe²,D-Pal³,D-Arg⁶,Dap(COCH₂S+Me₂)⁸,D-Ala¹⁰-LHRH andpharmaceutically acceptable salts thereof.
 32. A pharmaceuticalcomposition comprising a peptide compound of claim 1-31 and apharmaceutically acceptable carrier.
 33. A method of inhibiting LHRHactivity in a subject, comprising administering to a subject aneffective amount of a peptide compound of claim 1-31, such that LHRHactivity is inhibited.
 34. A method of inhibiting growth of ahormone-dependent tumor in a subject, comprising administering to asubject an effective amount of a peptide compound of claim 1-31, suchthat growth of the hormone-dependent tumor is inhibited.
 35. The methodof claim 34, wherein the hormone-dependent tumor is a prostate tumor.36. A method of inhibiting ovulation in a subject, comprisingadministering to a subject an effective amount of a peptide compound ofclaim 1-31, such that ovulation is inhibited.
 37. A packaged formulationfor treating a subject for a disorder associated with LHRH activity.comprising the peptide compound of claim 1-31 packaged with instructionsfor using the LHRH antagonist for treating a subject having a disorderassoClated with LHRH activity.
 38. A pharmaceutical compositioncomprising the peptide compound of claim 29 and a pharmaceuticallyacceptable carrier.
 39. The pharmaceutical composition of claim 38,which comprises a slow release polymer.
 40. The pharmaceuticalcomposition of claim 38, which is suitable for depot injection.
 41. Amethod of inhibiting LHRH activity in a subject, comprisingadministering to a subject an effective amount of the peptide compoundof claim 29, such that LHRH activity is inhibited.
 42. A method ofinhibiting growth of a hormone-dependent tumor in a subject, comprisingadministering to a subject an effective amount of the peptide compoundof claim 29, such that growth of the hormone-dependent tumor isinhibited.
 43. The method of claim 42, wherein the hormone-dependenttumor is a prostate tumor.
 44. A packaged formulation for treating asubject for a disorder assoClated with LHRH activity, comprising thepeptide compound of claim 29 packaged with instructions for using theLHRH antagonist for treating a subject having a disorder associated withLHRH activity.
 45. Use of the peptide compound of claim 1-31 in themanufacture of a medicament for the treatment of a disorder selectedfrom the group consisting of precoClous puberty, prostate cancer,ovarian cancer, benign prostatic hypertrophy, endometriosis, uterinefibroids, breast cancer, premenstrual syndrome, polycystic ovarysyndrome, and diseases which result from excesses of gonadal hormones.46. Use of the peptide of claim 29 in the manufacture of a medicamentfor the treatment of a disorder selected from the group consisting ofprecoClous puberty, prostate cancer, ovarian cancer, benign prostatichypertrophy, endometriosis, uterine fibroids, breast cancer,premenstrual syndrome, polycystic ovary syndrome, and diseases whichresult from excesses of gonadal hormones.
 47. The use of claim 46,wherein the disorder is prostate cancer.